EP1613684B1 - Procede de production de copolymeres de tetrahydrofurane - Google Patents

Procede de production de copolymeres de tetrahydrofurane Download PDF

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Publication number
EP1613684B1
EP1613684B1 EP04724282A EP04724282A EP1613684B1 EP 1613684 B1 EP1613684 B1 EP 1613684B1 EP 04724282 A EP04724282 A EP 04724282A EP 04724282 A EP04724282 A EP 04724282A EP 1613684 B1 EP1613684 B1 EP 1613684B1
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EP
European Patent Office
Prior art keywords
copolymerization
neopentyl glycol
water
thf
heteropolyacid
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
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EP04724282A
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German (de)
English (en)
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EP1613684A1 (fr
Inventor
Martin Haubner
Rolf Pinkos
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BASF SE
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BASF SE
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    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
    • C08G65/2642—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds characterised by the catalyst used
    • C08G65/2645—Metals or compounds thereof, e.g. salts
    • C08G65/2666—Hetero polyacids
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/04—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers only
    • C08G65/06—Cyclic ethers having no atoms other than carbon and hydrogen outside the ring
    • C08G65/16—Cyclic ethers having four or more ring atoms
    • C08G65/20—Tetrahydrofuran
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
    • C08G65/2696—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds characterised by the process or apparatus used

Definitions

  • the present invention relates to a novel process for the preparation of polyoxyalkylene glycols (Polyalkylenetherglykolen) by copolymerization of tetrahydrofuran - hereinafter called "THF" - with neopentyl glycol in the presence of heteropolyacids, is used in the pretreated neopentyl glycol.
  • THF tetrahydrofuran
  • Polyoxyalkylene glycols are important starting materials for the production of elastic fibers, elastic construction materials and coatings. They can be prepared inter alia by polymerization of THF or by copolymerization of THF with alpha, omega-diols such as neopentyl glycol - hereinafter referred to as "NPG" - in the presence of cationic catalysts. It is known, for example, from EP-A 126 471 to use heteropolyacids as catalysts.
  • Heteropolyacids are used in commercially available form either dried with a water content of 1 to 10 mol or undried with a water content of 10 to 40 mol of water per mole of heteropolyacid.
  • the rapid deactivation of the heteropolyacid catalyst proves to be particularly disadvantageous in the case of continuously conducted copolymerizations and processes with reused catalyst, since it leads to decreasing polymerization conversions.
  • the commercial grade neopentylglicol of the commercial grade is treated by methods known per se to reduce the total amount of organically bound nitrogen to below 5 ppm.
  • One way to purify technical grade neopentyl glycol alpha, omega-diols for use in the process of the invention is to recrystallize the neopentyl glycol from organic solvents.
  • Suitable organic solvents are C 1 to C 10 -alcohols, for example methane, ethanol, propanol or isopropanol, C 1 to C 10 ethers, for example tetrahydrofuran, diethyl ether, butylmethyl ether or halogenated solvents, such as chloroform or dichloromethane or mixtures thereof.
  • C 1 -C 10 -alcohols particularly preferably methanol.
  • the known layer or suspension crystallization in which the purification is achieved by crystallization from the melt and impurities remain in the melt, is also suitable.
  • neopentyl glycols used according to the invention is the solvent extraction of a saturated, aqueous, alcoholic or tetrahydrofuran-containing solution of neopentyl glycol with saturated or unsaturated aliphatic, cycloaliphatic or olefinic C 4 - to C 15 -hydrocarbons or C 4 - to C 15 ethers ,
  • hydrocarbons can also be used optionally containing halogen atoms such as chlorine.
  • mixtures of the abovementioned substance classes for extraction are suitable, which have a proportion of at least 50 wt .-% of the hydrocarbon or ether.
  • liquid-liquid extraction can be carried out in one or more stages, generally up to 5 stages, usually. Suitable apparatus and procedures are known to those skilled in the art and e.g. in "Ullmann's Encyclopedia of Industrial Chemistry, 6th Edition, Electronic Release". Discontinuous extractions can be carried out, for example, in the stirred tank. Examples of continuous extraction are the use of sieve tray columns, stirring columns and extraction batches, such as e.g. Mixer-settler. Membrane extractors, e.g. Hollow fiber modules can be used.
  • Suitable acidic ion exchangers are strongly acidic ion exchangers which contain sulfonic acid groups bound to an organic polymeric backbone via benzene groups, and for example in the form of the commercial products Amberlite® Ir 120, Amberjet® 1200 H and Duolite® C20 from Rohm & Haas Darmstadt, Dowex® HCR from Dow Chemical, Midland, Michigan, USA, Lewatit® K2621 and Lewatit® S100 from Bayer AG, Leverkusen, in all possible forms, for example granular or as a gel.
  • weakly acidic ion exchangers generally a polyacrylate, which are sold, for example, in the form of the commercial products Amberlite® IRC 76 and Duolite® C433, by the company Rohm & Haas, Darmstadt.
  • clays and zeolites in the H form.
  • the neopentyl glycol can be passed into the polymerization reactor via a prereactor filled with an ion exchanger.
  • the neopentyl glycol is passed in a mixture with THF and optionally a hydrocarbon and water ie the reaction medium of the polymerization, over the ion exchanger.
  • Tetrahydrofuran is in an amount of 40 to 99 wt.%, Based on the total amount of THF and alpha, omega-diol, preferably in an amount of 60 to 98 wt .-%, particularly preferably 80 to 97 wt .-%, in the copolymerization used.
  • the copolymerization according to the invention is preferably carried out in the presence of a hydrocarbon.
  • a hydrocarbon In the mixture with this hydrocarbon, water is distilled off from the copolymerization solution.
  • a hydrocarbon-water azeotrope Under mixture is understood in this application in addition to conventional non-azeotropic mixtures a hydrocarbon-water azeotrope. This procedure is described in the German Patent Application No. 102 399 47.6 dated 30.08.2002 BASF Aktiengesellschaft entitled “Process for the preparation of tetrahydrofuran copolymers", which is incorporated herein by reference.
  • the hydrocarbons used should be suitable for azeotrope formation with water.
  • the hydrocarbon for example, aliphatic or cycloaliphatic hydrocarbons having 4 to 12 carbon atoms or aromatic hydrocarbons having 6 to 10 carbon atoms or mixtures thereof are used.
  • the hydrocarbons are the fresh feed of the copolymerization in an amount of 1 x 10 -4 wt .-% (corresponding to 1 ppm) to 30% by weight, based on the fresh feed of alpha, omega-diol and THF, preferably 1 ppm to 16 wt .-%, particularly preferably 1 to 10 wt .-%, added.
  • the respective molecular weight can be adjusted.
  • 1 mole of heteropolyacid binds 10 to 40 molecules of water by coordinate bonding.
  • the heteropolyacids used as catalysts should contain about 1 to 10 molecules of water per molecule of heteropolyacid.
  • water is released by the copolymerization with the neopentyl glycol used as a comonomer. The higher the water content of the copolymerization solution, the lower the molecular weight of the resulting copolymer.
  • average molecular weight or “average molecular weight” in this application means the number average Mn of the molecular weight of the polymers contained in the polymer formed.
  • Heteropolyacids which are used according to the invention are inorganic polyacids which, in contrast to isopolyacids, have at least two different central atoms.
  • Heteropoly acids are formed from weak polybasic oxygen acids of a metal such as chromium, molybdenum, vanadium and tungsten and a nonmetal such as arsenic, iodine, phosphorus, selenium, silicon, boron and tellurium as partial mixed anhydrides. Examples include the dodecatungstophosphoric acid H 3 (PW 12 O 40 ) or the decamolybdophosporic acid H 3 (PMo 12 O 40 ).
  • the heteropolyacids may also contain actinides or lanthanides as the second central atom (Z. Chemie 17 (1977), pages 353 to 357 and 19 (1979), 308).
  • the heteropolyacids can generally be described by the formula H 8 -n (Y n M 19 O 40 ) where n is the valency of the element Y (eg boron, silicon, zinc) (see also Heteropoly- and Isopolyoxomtalates, Berlin, Springer 1983).
  • Suitable catalysts for the process according to the invention are phosphotungstic acid, phosphomolybdic acid, silicon molybdic acid and silicotungstic acid.
  • heteropolyacids used as catalysts can be used both dried (1 to 10 moles of water / mole heteropolyacid) or undried (10 to 40 moles of water / heteropolyacid) in the copolymerization.
  • the water present in the copolymerization reactor which is partly water of crystallization of the heteropolyacid and partly of water formed during the reaction, is obtained as a mixture of the hydrocarbon added with the fresh feed with water at a temperature of 40 to 120 ° C, especially preferably from 50 to 70 ° C and a pressure of 150 mbar to 2 bar, preferably 230 mbar by means of a conventional distillation device directly from the copolymerization, that is separated from the copolymerization without intermediate processing steps such as phase separations.
  • the resulting vapor is preferably deposited in a surface condenser; however, quench and injection capacitors are also possible.
  • the resulting condensate is fed to the elimination of the water of the solvent processing.
  • a partial recycling of the condensate into the reactor, ie a removal of the heat of reaction by means of evaporative cooling, is particularly favorable.
  • To achieve the highest possible water content in deducting condensate can between reactor and condenser is still a multi-stage, be inserted with the recycle condensate as reflux countercurrent rectification column.
  • THF is distilled off simultaneously with the mixture of the hydrocarbon used in the copolymerization with water, which can form a ternary azeotrope depending on the hydrocarbon.
  • the hydrocarbon distilled off in a mixture with water or the mixtures of water and hydrocarbon with tetrahydrofuran can be dried with a suitable solid adsorbent, for example on molecular sieves, and recycled again to the copolymerization.
  • a phase separation into an aqueous phase and the hydrocarbon is conceivable.
  • the aqueous phase contains up to 5% by weight of THF, preferably ⁇ 1% by weight. It also contains in concentrations ⁇ 1% by weight of the respective hydrocarbon. THF and the hydrocarbon can be recovered by distillation of the aqueous phase and recycled. However, the aqueous phase can also be discarded.
  • the remaining after the separation of the hydrocarbon / water mixture copolymer solution is preferably converted into a phase separator.
  • the heteropolyacid is separated from the product phase.
  • the heteropolyacid is preferably reused for the next copolymerization. This process, known for example from EP-A 181 621, leads to the precipitation of the heteropolyacid from the organic phase.
  • the hydrocarbon used is preferably the hydrocarbon already used in the copolymerization.
  • the heteropolyacid is preferably reused for the next copolymerization.
  • the process of the invention can be carried out both continuously and batchwise as well as in a semi-batch mode.
  • Semi-batch operation or semi-continuous operation is understood to mean that the heteropolyacid is initially charged with 20 to 50% by weight of the other starting materials. In the course of the reaction time, the remaining residue of the educts is then added.
  • the heteropolyacid is suitably used in amounts of from 1 to 300 parts by weight, preferably from 5 to 150 parts by weight, based on 100 parts by weight of the monomers used (THF and neopentyl glycol). It is also possible to add larger amounts of heteropolyacid to the reaction mixture.
  • the heteropolyacid may be fed to the reaction in solid form, whereupon it is gradually formed by contacting with the other reactants the liquid catalyst phase is solvated. It is also possible to proceed by mashing the solid heteropolyacid with the neopentyl glycol and / or the THF and passing the catalyst solution obtained as the liquid catalyst phase into the reactor. In this case, both the catalyst phase and the monomeric starting material can be initially charged in the reactor. However, it is also possible for both components to be introduced simultaneously into the reactor.
  • Water is in a continuous procedure in an amount of 0.1 to 5 wt .-%, preferably 0.1 to 3.5 wt .-%, particularly preferably 0.1 - wt .-%, based on the total amount of monomer THF and comonomer, usually metered via a level control metered into the reactor.
  • fresh monomer is supplied as the product and unreacted monomer are discharged from the reaction apparatus.
  • the residence time thus the polymerization time, can be controlled, thus providing a further means for influencing and adjusting the average molecular weight and the molecular weight distribution of the resulting polymer.
  • the copolymerization can be monitored and controlled by online conductivity measurement.
  • Interruption of the copolymerization in batch mode is preferred in a conductivity range between 0.1-2.5 ⁇ S, depending on the desired target molecular weight.
  • these 10 - 500 ppm, particularly preferably 50 - 300 ppm of a radical scavenger can be added.
  • Particularly suitable radical scavengers are 250 ppm of 2,6-di-tert-butyl-4-methyl-cresol (BHT).
  • the copolymerization is carried out depending on the amount of the catalyst and the reaction temperature in the batch process for a period of from 0.5 to 70 hours, preferably from 5 to 50 hours and more preferably from 10 to 40 hours.
  • residence times of from 1 to 50 and preferably from 10 to 40 hours are usually set.
  • the reaction system described requires a certain time until a steady state equilibrium has been established and during it may be advantageous to keep the reactor outlet closed, so carry out any product solution from the reaction apparatus.
  • the copolymerization is usually carried out at temperatures of 20 to 100 ° C, preferably at 30 to 80 ° C.
  • it is carried out under atmospheric pressure, the reaction under pressure, especially under the autogenous pressure of the reaction system, but may also prove to be useful and advantageous.
  • the reactors should be equipped with powerful mixing devices, such as agitators, in both batch, semi-batch and continuous operations.
  • inventive method is advantageously carried out under an inert gas atmosphere, wherein any inert gases, such as nitrogen or argon, can be used.
  • any inert gases such as nitrogen or argon
  • the reactants are freed before use from any water and peroxides contained therein.
  • reaction in conventional, suitable for continuous process reactors or reactor arrangements, for example in tubular reactors, which are equipped with internal fittings that ensure a thorough mixing of emulsion-like Copolymerisationsansatzes or else be carried out in stirred tank cascades.
  • An emulsion-like copolymerization mixture is understood to mean one at water contents of 2 to 10 mol of water / per mole of heteropolyacid.
  • polyoxyalkylene glycols can be produced economically, without loss of catalyst activity and in good yield, selectively and with a narrow molecular weight distribution and in pure form with lower color numbers.
  • the copolymers have incorporation rates of the neopentyl glycol comonomer of from 5 to 50% by weight, based on the copolymer, and average molecular weights M n of from 600 to 6,000.
  • the polyoxyalkylene glycols which can be prepared according to the invention are used, for example, for the preparation of special polyurethanes which are suitable as highly elastic composite materials.
  • a polyurethane polymer containing the copolymers which can be prepared according to the invention has a high elongation after breakage, a small change in elongation, a small loss of hysteresis during expansion and contraction, and high elasticity even in extreme cold.
  • the hydroxyl number is understood as meaning that amount of potassium hydroxide in mg which is equivalent to the amount of acetic acid bound in the acetylation of 1 g of substance.
  • the hydroxyl number is determined by the esterification of the hydroxyl groups present with an excess of acetic anhydride. After the reaction, the excess acetic anhydride is hydrolyzed with water and back titrated as acetic acid with sodium hydroxide solution.
  • the continuously obtained reaction product of the polymerization reactor was admixed with 250 g of pentane and subjected to phase separation.
  • the heavy catalyst phase was recycled to the polymerization reactor.
  • the upper phase was run at 20 ° C over a combination of cation and anion exchangers, which were each arranged as a fixed bed.
  • Example 1 was repeated analogously to commercially available NPG of technical grade (content of organically bound nitrogen 15 ppm), but the pre-reactor filled with ion exchanger was removed.
  • the copolymerization conversion determined by sampling was 37% at the beginning of the experiment. Within a test period of 2000 h, the catalyst deactivated strongly. After 2000 hours of operation, the average polymerization conversion was 30.6%. This corresponds to a mean deactivation of about 0.08% / day.

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  • Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Organic Chemistry (AREA)
  • Polyethers (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (6)

  1. Procédé de préparation en une étape de polyoxyalkylèneglycols par copolymérisation de THF et de néopentylglycol en présence d'un hétéropolyacide, caractérisé en ce que la teneur en azote organiquement fixé dans le néopentylglycol est inférieure à 5 ppm.
  2. Procédé de préparation en une étape de polyoxyalkylèneglycols suivant la revendication 1, caractérisé en ce que la teneur du néopentyglycol en azote organiquement fixé est obtenue par traitement de néopentylglycol de qualité technique par recristallisation, extraction par un solvant ou traitement avec un échangeur d'ions.
  3. Procédé de préparation en une étape de polyoxyalkylèneglycols suivant l'une des revendications 1 et 2, caractérisé en ce que 3 à 20 % en poids de néopentylglycol sont, par rapport au tétrahydrofurane, mis en oeuvre.
  4. Procédé de préparation en une étape de polyoxyalkylèneglycols, suivant l'une des revendications 1 à 3, caractérisé en ce que la copolymérisation est effectuée en présence d'un hydrocarbure.
  5. Procédé de préparation en une étape de polyoxyalkylèneglycols suivant l'une des revendications 1 à 4, caractérisé en ce que le procédé est conduit en continu.
  6. Procédé de préparation en une étape de polyoxyalkylèneglycols suivant l'une des revendications 1 à 5, caractérisé en ce que la copolymérisation est effectuée à des températures de 20 à 100°C.
EP04724282A 2003-04-01 2004-03-30 Procede de production de copolymeres de tetrahydrofurane Expired - Lifetime EP1613684B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10314648A DE10314648A1 (de) 2003-04-01 2003-04-01 Verfahren zur Herstellung von Tetrahydrofuran-Copolymeren
PCT/EP2004/003336 WO2004087786A1 (fr) 2003-04-01 2004-03-30 Procede de production de copolymeres de tetrahydrofurane

Publications (2)

Publication Number Publication Date
EP1613684A1 EP1613684A1 (fr) 2006-01-11
EP1613684B1 true EP1613684B1 (fr) 2006-06-28

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EP04724282A Expired - Lifetime EP1613684B1 (fr) 2003-04-01 2004-03-30 Procede de production de copolymeres de tetrahydrofurane

Country Status (11)

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US (1) US7361793B2 (fr)
EP (1) EP1613684B1 (fr)
JP (1) JP2007534776A (fr)
KR (1) KR101021738B1 (fr)
CN (1) CN100362041C (fr)
AT (1) ATE331750T1 (fr)
DE (2) DE10314648A1 (fr)
ES (1) ES2268652T3 (fr)
MY (1) MY137273A (fr)
TW (1) TWI339212B (fr)
WO (1) WO2004087786A1 (fr)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102004012116A1 (de) * 2004-03-12 2005-09-22 Basf Ag Verfahren zur Herstellung von Polytetrahydrofuran oder Tetrahydrofuran-Copolymeren
JP7155810B2 (ja) * 2018-09-26 2022-10-19 コニカミノルタ株式会社 トナー補給装置、現像装置および画像形成装置
WO2021001920A1 (fr) * 2019-07-02 2021-01-07 三菱ケミカル株式会社 Composition de polyalkylène éther glycol et son procédé de production
CN115109247A (zh) * 2022-08-02 2022-09-27 南京理工大学 一种含有甲基侧链的四氢呋喃-乙二醇共聚醚及其合成方法

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1216597A (fr) * 1983-05-23 1987-01-13 Atsushi Aoshima Production de polyetherglycole
JPS61123626A (ja) * 1984-11-21 1986-06-11 Asahi Chem Ind Co Ltd 分子中にポリオキシアルキレン基を有する重合体の製造方法
JPH0713139B2 (ja) * 1984-03-28 1995-02-15 旭化成工業株式会社 ポリエーテルポリオール共重合体の製造方法
DE3563447D1 (en) * 1984-03-28 1988-07-28 Asahi Chemical Ind Process for producing polyether polyol, the produced polyether polyol and polyurethane
CA1268481A (fr) 1984-11-13 1990-05-01 Atsushi Aoshima Epuration du polyether
JPH1087813A (ja) * 1996-09-12 1998-04-07 Asahi Chem Ind Co Ltd 共重合ポリエーテルポリオールの精製方法
CN1083413C (zh) * 1996-10-22 2002-04-24 株式会社Lg化学 新戊二醇的连续生产方法
TW444032B (en) 1998-06-15 2001-07-01 Asahi Chemical Ind Process for producing tetrahydrofuran polymer
JP2002012568A (ja) * 2000-06-27 2002-01-15 Mitsubishi Gas Chem Co Inc ネオペンチルグリコールの精製法
EP1361243B1 (fr) * 2001-01-11 2010-11-24 Asahi Kasei Fibers Corporation Copolymere d'oxytetramethylene glycol et son procede de production

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Publication number Publication date
KR20060006907A (ko) 2006-01-20
KR101021738B1 (ko) 2011-03-15
ATE331750T1 (de) 2006-07-15
ES2268652T3 (es) 2007-03-16
US20060258837A1 (en) 2006-11-16
CN1802401A (zh) 2006-07-12
CN100362041C (zh) 2008-01-16
US7361793B2 (en) 2008-04-22
DE502004000892D1 (de) 2006-08-10
DE10314648A1 (de) 2004-10-14
EP1613684A1 (fr) 2006-01-11
TW200504118A (en) 2005-02-01
WO2004087786A1 (fr) 2004-10-14
TWI339212B (en) 2011-03-21
JP2007534776A (ja) 2007-11-29
MY137273A (en) 2009-01-30

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